CN111186953A - Thermal desulfurization wastewater zero discharge system and method - Google Patents
Thermal desulfurization wastewater zero discharge system and method Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
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Abstract
The invention relates to the field of desulfurization wastewater treatment, in particular to a thermal desulfurization wastewater zero-discharge system and process. The utility model provides a desulfurization waste water zero release system, first effect heater (9) top is connected with first effect separator (10), the upper portion and the low temperature economizer (1) of first effect heater (9) are connected, the lower part and the waste water tank (2) of first effect separator (10) are connected, the bottom of first effect separator (10) and the bottom of first effect heater (9) are passed through the circulating pump and are connected. The invention has simple integral process, high reliability and low maintenance and operation cost, and the high-temperature bypass flue gas returns to the main flue after evaporating the waste water without additionally increasing the smoke quantity. The technology has the advantages of no problems of large pretreatment dosage and insufficient sludge generation, process flow can be simplified, and automatic stable operation is realized. In addition, the process can effectively avoid the phenomenon that the flue is blocked by the deposited dust, and improve the running stability of the unit.
Description
Technical Field
The invention relates to the field of desulfurization wastewater treatment, in particular to a thermal desulfurization wastewater zero-discharge system and process.
Background
At present, domestic power plant desulfurization wastewater is recycled after being treated by conventional primary treatment, and still has a plurality of problems. The waste water treatment → dosing → sludge treatment process is a common process for desulfurizing waste water. The method has the advantages of large dosage, high cost, large subsequent sludge treatment capacity, low efficiency and long period. After the conventional treatment, although the discharge index is met, the salt content of the wastewater is still high, and heavy metals still exist, so that the aim of zero discharge cannot be achieved. If the dry ash is selected for being reused for humidifying dry ash and spraying in a coal yard, the quality of the dry ash and the quality of the coal yard are affected, and the direct discharge can cause harm to the environment. According to the water supply professional water balance, other industrial wastewater and domestic sewage and the like in the plant can be treated, recycled and consumed in the power plant, the circulating water sewage is used as the process water of the desulfurization system, and only the desulfurization wastewater is too high in salt content and basically cannot be utilized, so that the method becomes the biggest difficulty for realizing zero discharge of the wastewater in the coal-fired power plant. Therefore, the desulfurization wastewater must adopt an advanced treatment scheme to thoroughly solve the problem of the recycling way, and realize zero emission treatment in the real sense, namely no waste liquid and no waste solids. The existing flue gas waste heat concentration technology is a treatment scheme for atomizing and concentrating desulfurization waste water in a flue from a dust remover to the front of a wet desulfurization absorption tower. This can lead to the occurrence of ash deposition blocking the flue, and threatens the stable operation of the unit. Therefore, the development of the desulfurization wastewater zero-discharge method suitable for industrial application has wide economic and social benefits.
Disclosure of Invention
The invention aims to provide a low-cost thermal desulfurization wastewater zero-discharge process scheme, which combines a multi-effect flash evaporation technology and a high-temperature bypass flue gas evaporation technology and can solve the problems in the background technology.
In order to achieve the above object, the present invention adopts the following technical solutions (claims):
the technical scheme adopted by the patent to solve the technical problem
A desulfurization wastewater zero-discharge system comprises a low-temperature economizer, a wastewater tank, a feed pump, a multi-effect flash system, a concentrated water tank, a triple box, a bypass evaporation chamber, a fan, a thickening tank and a vacuum pump, wherein the multi-effect flash system comprises a first effect separation system, a second effect separation system and a third effect separation system; the first effect separation system, the second effect separation system and the third effect separation system are all composed of heaters and separators, wherein the top of the first effect heater is connected with the first effect separator, the upper part of the first effect heater is connected with the low-temperature economizer, the lower part of the first effect separator is connected with the wastewater tank, and the bottom of the first effect separator is connected with the bottom of the first effect heater through a circulating pump; the arrangement of the second effect separation system and the third effect separation system is the same as that of the first effect separation system; the third effect separation system is connected with a thickening tank, and the thickening tank is connected with a concentration water tank through a discharge pump; the concentrated water tank is connected with the triple water tank, and the triple water tank is connected with the bypass evaporation chamber.
Preferably, the concentrate tank employs a pulsed suspension device.
Preferably, the bypass evaporation chamber is a sprayer, and the sprayer consists of a nozzle and a spray gun; the system is provided with a moisture monitoring device at the position where the bypass evaporation chamber converges into the main flue, and the moisture monitoring device can automatically adjust the amount of waste water or shut down the flue evaporation spraying device once continuous alarm occurs.
A zero-emission process of the system comprises the following steps:
(1) the desulfurization wastewater enters a first-effect separation system, the desulfurization wastewater is heated in a first-effect heater by the heat of a low-temperature economizer and spirally flows from bottom to top on the inner wall of a pipe, and the boiling desulfurization wastewater enters a first-effect separator to complete vapor-liquid separation;
(2) the desulfurization wastewater is circulated for many times in the first-effect system, flash evaporation concentration is completed, and preliminary concentration is completed and then the desulfurization wastewater enters a second-effect separation system;
(3) the desulfurization wastewater circulates in the second-effect system, flash evaporation concentration is completed, then the desulfurization wastewater is sent into the third-effect system for circulation, flash evaporation concentration is performed in the third-effect separation system, and the concentrated desulfurization wastewater enters a thickening tank;
(4) concentrated liquid in the thickening tank is input into a concentration water tank through a discharge pump, concentrated wastewater in the concentration water tank is introduced into a triple box treatment system for clarification and filtration, and the clarified wastewater is introduced into a high-temperature bypass flue gas evaporation system for evaporation to dryness;
(5) the flue gas in the bypass evaporation chamber enters the flue.
Preferably, the concentration of the desulfurization wastewater in the step (2) after circulating in the first effect system and completing flash evaporation concentration is 10% -15.5%; the concentration of the mixture which circulates in the second effect system and is subjected to flash evaporation concentration in the step (3) is 20% -27%; and (3) the concentration of the flash evaporation, concentration and concentration in the third-effect separation system is 45-55%.
Preferably, the temperature of the first effect separation system is 95 ℃ and the absolute pressure is 75.61 Kpa; the temperature of the second-effect separation system is 85 ℃, and the absolute pressure is 38.56 Kpa; the temperature of the third effect separation system was 68 ℃ and the absolute pressure was 15.8 Kpa.
Preferably, the temperature of the steam at the outlet of the low-temperature economizer in the step (1) is about 108 ℃, the pressure is 95KPa, and the flow rate is 8 t/h.
The invention has simple integral process, high reliability and low maintenance and operation cost, and the high-temperature bypass flue gas returns to the main flue after evaporating the waste water without additionally increasing the smoke quantity. The technology has the advantages of no problems of large pretreatment dosage and insufficient sludge generation, process flow can be simplified, and automatic stable operation is realized. In addition, the process can effectively avoid the phenomenon that the flue is blocked by the deposited dust, and improve the running stability of the unit.
The desulfurization wastewater zero-discharge system provided by the invention can extract hot flue gas with different proportions according to different wastewater treatment capacities, so that the desulfurization wastewater can be completely evaporated, and the evaporation is not influenced by boiler load. The technology has low investment and operation cost, can be used as a terminal for treating wastewater of a power plant, and really realizes zero emission of wastewater of the power plant, but the bypass evaporation process has certain influence on the thermal efficiency of a boiler due to the fact that a high-grade heat source before an air preheater is extracted, so that the desulfurization wastewater is reduced by a pre-concentration process, and the total evaporation amount of the desulfurization wastewater is reduced.
Advantageous effects
(1) The amount of the desulfurization waste water in the concentration stage is reduced, the salt concentration is increased, the evaporation energy consumption of the front-end high-temperature flue gas is reduced, and the effects of fully utilizing the waste heat of the flue gas of the power plant and fully ensuring zero emission are achieved.
(2) In order to prevent the crystal from depositing in the tank, the concentrated water tank adopts a pulse suspension device, slurry is pumped out of the water tank body by a pulse suspension pump and is sprayed to the bottom of the tank through a pulse suspension pipe arranged in the tank, so that the effect of stirring the slurry is achieved. The device has the advantages that no mechanical rotating part is arranged in the slurry, and the problem that the propeller needs to be stopped, drained and overhauled when the propeller fails is solved.
(3) The bypass system in the high-temperature bypass flue gas evaporation system avoids the safety problems of corrosion and ash blockage of a flue, blockage of a dust remover and the like, and the complete set of device is completely independent. The bypass is separated from the host, so that the online maintenance is easy, and potential safety hazards are avoided.
Drawings
FIG. 1 is a flow diagram of desulfurized wastewater;
FIG. 2 is a schematic view of a desulfurization waste water flash;
FIG. 3 is a view of the sprayer;
in the figure: 1. a low-temperature economizer; 2. a wastewater tank; 3. a feed pump; 4. a multi-effect flash system; 5. A concentrated water tank; 6. a triple header; 7. a bypass evaporation chamber; 8. a fan; 9. a first effect heater; 10. a first effect separator; 11. a second effect heater; 12. a second effect separator; 13. a third effect heater; 14. a third effect separator; 15. a thickening tank; 16. 17, a vacuum pump; 18. a spray gun; 19. a nozzle; 20. a flue.
Detailed Description
To further illustrate the technical means and effects adopted by the present invention to achieve the predetermined objects, the following description will be made in conjunction with the accompanying drawings and preferred embodiments of a drying and solidifying tower for zero discharge of wastewater, the specific implementation, structure, characteristics and effects thereof according to the present invention.
Example 1
A desulfurization wastewater zero-discharge system comprises a low-temperature economizer 1, a wastewater tank 2, a feeding pump 3, a multi-effect flash system 4, a concentrated water tank 5, a triple box 6, a bypass evaporation chamber 7, a fan 8, a thickening tank 15 and a vacuum pump 16, wherein the multi-effect flash system 4 comprises a first-effect separation system, a second-effect separation system and a third-effect separation system; the first effect separation system, the second effect separation system and the third effect separation system are all composed of heaters and separators, wherein the top of a first effect heater 9 is connected with a first effect separator 10, the upper part of the first effect heater 9 is connected with a low-temperature economizer 1, the lower part of the first effect separator 10 is connected with a wastewater tank 2, and the bottom of the first effect separator 10 is connected with the bottom of the first effect heater 9 through a circulating pump; the arrangement of the second effect separation system and the third effect separation system is the same as that of the first effect separation system; the third-effect separation system is connected with a thickening tank 15, and the thickening tank 15 is connected with the concentration water tank 5 through a discharge pump; the concentrated water tank 5 is connected with the triple water tank 6, and the triple water tank 6 is connected with the bypass evaporation chamber 7; the concentrated water tank (5) adopts a pulse suspension device;
the bypass evaporation chamber 7 is a sprayer which is composed of a nozzle (19) and a spray gun (18).
A zero-emission process of the system comprises the following steps:
(1) enabling the desulfurization wastewater to enter a first effect separation system, wherein the temperature of the first effect separation system is 95 ℃, the absolute pressure is 75.61Kpa, the desulfurization wastewater is heated in a first effect heater by the heat of a low-temperature economizer, the temperature of steam at an outlet of the low-temperature economizer is about 108 ℃, the pressure is 95KPa, and the flow is 8 t/h; spirally flows from bottom to top on the inner wall of the pipe, and the boiled desulfurization wastewater enters a first effect separator to complete the separation of vapor and liquid;
(2) the desulfurization wastewater is circulated for multiple times in the first effect system and is subjected to flash evaporation concentration, and the desulfurization wastewater enters the second effect separation system when the concentration of the desulfurization wastewater after being circulated in the first effect system and subjected to flash evaporation concentration is 10-15.5%; (3) the desulfurization wastewater circulates in the second-effect system and is subjected to flash evaporation concentration, the temperature of the second-effect separation system is 85 ℃, the absolute pressure is 38.56Kpa, and the concentration after the flash evaporation concentration is 20% -27% is sent into the third-effect system for circulation; carrying out flash evaporation concentration in a third-effect separation system, wherein the temperature of the third-effect separation system is 68 ℃, the absolute pressure is 15.8Kpa, and the desulfurized wastewater with the concentration of 45-55% after flash evaporation concentration enters a thickening tank;
(4) the concentrated liquid in the thickening tank is input into a concentrated water tank through a discharge pump, and the volume of the concentrated water tank is selected to be 75m3(phi 4000X 6000). In order to prevent the crystal from depositing in the tank, the concentrated water tank adopts a pulse suspension device, slurry is pumped out of the water tank body by a pulse suspension pump and is sprayed to the bottom of the tank through a pulse suspension pipe arranged in the tank, so that the effect of stirring the slurry is achieved. The device has the advantages that no mechanical rotating part exists in slurry, the problem that the propeller needs to be stopped to discharge slurry for maintenance when the propeller breaks down does not exist, the pulse suspension pipeline is made of FRP materials and horizontally arranged at the bottom of the concentrated water tank, and the pulse suspension pipeline is fixed by the supporting beam. And a solid conical pulse suspension spray pipe is arranged on the pulse suspension pipeline and is made of silicon carbide. The concentrated waste water is conveyed to a triple box through a pump for clarification and filtration, and is conveyed to a bypass evaporation chamber for evaporation after being treated. Introducing the concentrated wastewater in the concentrated water tank into a triple box treatment system for clarification and filtration, and introducing the clarified wastewater into a high-temperature bypass flue gas evaporation system for evaporation;
(5) high-temperature flue gas is led to the bypass evaporation chamber from the denitration outlet through the fan to evaporate desulfurization waste water, and concentrated desulfurization waste water is all evaporated in the high-temperature bypass evaporation chamber. And the bypass evaporation chamber takes flue gas from the denitration outlet flue and then converges the flue gas into the rear flue of the air preheater. The high-temperature bypass system is designed to be a sprayer with smaller spray particle size and mainly comprises a nozzle and a spray gun, and the spray gun is provided with a flange for fixing, as shown in figure 3. The system is provided with a moisture monitoring device at the position where the bypass evaporation chamber converges into the main flue, and the moisture monitoring device can automatically adjust the amount of waste water or shut down the flue evaporation spraying device once continuous alarm occurs.
Claims (7)
1. A thermal desulfurization wastewater zero-discharge system comprises a low-temperature economizer (1), a wastewater tank (2), a feeding pump (3), a multi-effect flash evaporation system (4), a concentrated water tank (5), a triple box (6), a bypass evaporation chamber (7), a fan (8), a thickening tank (15) and a vacuum pump (16), and is characterized in that the multi-effect flash evaporation system (4) comprises a first-effect separation system, a second-effect separation system and a third-effect separation system; the first effect separation system, the second effect separation system and the third effect separation system are all composed of heaters and separators, wherein the top of the first effect heater (9) is connected with the first effect separator (10), the upper part of the first effect heater (9) is connected with the low-temperature economizer (1), the lower part of the first effect separator (10) is connected with the wastewater tank (2), and the bottom of the first effect separator (10) is connected with the bottom of the first effect heater (9) through a circulating pump; the arrangement of the second effect separation system and the third effect separation system is the same as that of the first effect separation system; the third-effect separation system is connected with a thickening tank (15), and the thickening tank (15) is connected with the concentration water tank (5) through a discharge pump; the concentrated water tank (5) is connected with the triple water tank (6), and the triple water tank (6) is connected with the bypass evaporation chamber (7).
2. System according to claim 1, characterized in that the concentrate tank (5) employs a pulsed suspension device.
3. System according to claim 1, characterized in that the bypass evaporation chamber (7) is provided with a sprayer consisting of a nozzle (19) and a spray gun (18).
4. A zero-emission process with a system according to claims 1-3, characterized by the following steps:
(1) the desulfurization wastewater enters a first-effect separation system, the desulfurization wastewater is heated in a first-effect heater by the heat of a low-temperature economizer and spirally flows from bottom to top on the inner wall of a pipe, and the boiling desulfurization wastewater enters a first-effect separator to complete vapor-liquid separation;
(2) the desulfurization wastewater is circulated for many times in the first-effect system, flash evaporation concentration is completed, and preliminary concentration is completed and then the desulfurization wastewater enters a second-effect separation system;
(3) the desulfurization wastewater circulates in the second-effect system, flash evaporation concentration is completed, then the desulfurization wastewater is sent into the third-effect system for circulation, flash evaporation concentration is performed in the third-effect separation system, and the concentrated desulfurization wastewater enters a thickening tank;
(4) concentrated liquid in the thickening tank is input into a concentration water tank through a discharge pump, concentrated wastewater in the concentration water tank is introduced into a triple box treatment system for clarification and filtration, and the clarified wastewater is introduced into a high-temperature bypass flue gas evaporation system for evaporation to dryness;
(5) the flue gas in the bypass evaporation chamber enters the flue.
5. The zero-emission process of claim 4, wherein the concentration of the desulfurization wastewater in the step (2) after circulating in the first effect system and performing flash evaporation concentration is 10% -15.5%; the concentration of the mixture which circulates in the second effect system and is subjected to flash evaporation concentration in the step (3) is 20% -27%; and (3) the concentration of the flash evaporation, concentration and concentration in the third-effect separation system is 45-55%.
6. The zero-emission process of claim 4, wherein the first effect separation system has a temperature of 95 ℃ and an absolute pressure of 75.61 Kpa; the temperature of the second-effect separation system is 85 ℃, and the absolute pressure is 38.56 Kpa; the temperature of the third effect separation system was 68 ℃ and the absolute pressure was 15.8 Kpa.
7. The process of claim 4, wherein the temperature of the low-temperature economizer outlet steam in the step (1) is about 108 ℃, the pressure is 95KPa, and the flow rate is 8 t/h.
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Cited By (1)
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| CN111892112A (en) * | 2020-08-31 | 2020-11-06 | 中电华创电力技术研究有限公司 | Treatment system for zero discharge of desulfurization wastewater of coal-fired power plant |
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